JPS5869709A - Method and apparatus for activating and reactivating particularly active carbon for carrying out gas/solid reaction - Google Patents

Abstract

(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method and apparatus for carrying out gas/solid-state reactions, in particular for activating and reactivating activated carbon.

It is known to activate carbon-containing raw materials. Various types of furnaces are used for this purpose.5 However, only three of these furnaces are generally required: direct-heat rotary furnaces, multistage furnaces, and fluidized bed furnaces. It is a furnace.

Direct heating rotary furnaces - whose structural integrity has long proven their utility in other high temperature applications - are probably the first and most frequently used large-scale furnaces. It is probably an industrial activation device. In this furnace,
The transport of the gasifying agent and the transport of the reactor must take place via the surface of the carbon bed that is in contact with the gas body, while the removal of the reaction residue must take place through the same cross section.

This surface is therefore considered the most important factor that governs the rotary tube technology and to which extent the surface regeneration can be enhanced and moderated (e.g. by increasing the rotational speed, incorporating vanes).
Ohem by H. Helmrich et al.

Ing, Techn, Vol. 51 (1979), No. 8,
771 pages and T. K. Brimacombe et al., Metallurgical Transaction.
ns vol. 93 (1978), p. 201).

The multistage furnace is a type of furnace that has only recently come into use for the production and reactivation of carbonaceous materials (U.S. Patent No. 3.
994.829). The furnace consists of a vertical enclosure divided into individual stages by an enclosed bottom.
It consists of a cylindrical casing. .

The carbon material charged at the top is fed through the bottom, flowing alternately from inside to outside and vice versa, and the horizontal feed of the carbon material falling through the holes onto the bottom lying below is It is carried out with a plow-shaped blade fixed to an arm that rotates itself.

, fL, the activating gas heated to a high temperature that does not reach the level of surface infiltration is introduced at the bottom and is guided in countercurrent to the carbonaceous material from one stage to another. Each stage is heated by an auxiliary burner and/or an additional steamer or secondary air is introduced.

The disadvantage of this multi-stage furnace is that it has a complicated mechanism.

In order to increase the exchange surface between the carbonaceous material and the reactant gas, it is easily conceivable to allow the gas to flow through the carbonaceous bed. This process is carried out in a fixed bed or a fluidized bed.

Moreover, this known cylindrical fluidized bed furnace is not suitable for activating carbonaceous materials. Because this furnace has a very unfavorable retention spectrum - T:I The residence time behavior of individual particles is not important. On the other hand, the activation process is performed under the same activation conditions (temperature, residence time,
This is a partial waste ratio process that emphasizes placing the product under (H2O-partial pressure). Uniform temperature distribution and good partial pressure equilibrium due to intensive mixing are essential features of fluidized beds. However, as a result of the chaotic remixing within the cylindrical vortex bed, only about 65% of the solids are carried away after a moderate residence time, while at least 10% of the solids are transported away. Remains in the same state in the vortex bed for three times as long as the residence time (H. Juntgen et al., C!hem, ■ng, Teahn, vol. 49 (19
77), No. 2, MS 447/77) - however, different residence times create conditions for different combustion in the individual particles and thus an increase in the quality spectrum.

For this purpose, the decisive effect of the retention spectrum on the activation of carbonaceous materials in the fluidized bed is discussed in 1.
It is clear from the fact that 5 one-stage circular reactors are known (J, K], ein Ohem Eng, Techn.
, Vol. 51 (1979), No. 4 MS 680/'79).

In order to avoid uncontrolled remixing, various solutions are available, such as dividing the reactor into a number of individual fluidized beds, which are connected one after the other in a cascade and placed in a common reactor. is proposed.

Another solution is known from Yoneyama patent % 3.976.597. In this case, the swirling fluidized bed is formed as a rectangular groove in which the fluidized carbonaceous material is -
As much as possible, the piston flow is transferred from the primary inlet to the outlet.

The transfer is carried out by pushing out the harmful substances in the bed by the loaded carbonaceous material volume. By splitting the groove into two or many single grooves, the residence time spectrum is further narrowed.

A further development of this method is the BV-vortex fluidized bed reactor (see US Pat. No. 4,058,374). In this method, the single grooves are not provided one after the other, but one above the other, and the fluidizing gas sequentially passes through the single vortex fluidized bed. Flow. In a single groove, a dam plate immersed into the bed from above prevents remixing. 'The disadvantage of these fluidized bed techniques is that the fluidizing gas must act on the one hand as the reaction sludge and on the other hand entrain the heat necessary for the endothermic sludge reaction. Therefore, only the top gas should be used as fluidizing medium, the temperature of which is higher than the activation temperature, corresponding to the heat consumption of the reaction. However, the use of the top gas as fluidizing gas means that water vapor partial pressures of up to 0.5-0.4 can be reached to maintain it in suspension within the 8-vortex sliding bed. requires a fully defined minimum fluidization rate which factors in the density of the gas (which varies with temperature), the bulk density of the carbon material (which decreases during the course of activation), and the grain size of the carbon material. be.

(The interdependence of the elements 1c and I suggests that the optimal adjustment of this fluidized bed technology is not straightforward.) Other fluidized bed reactors are known from German Patent Application No. 2 615 1437. .

Useless remixing effects are avoided in this reactor due to the relatively large quotient/diameter ratio and by the fact that the carbonaceous material is fed through pipes extending all the way to the grid and discharged along the fluidized bed surface. Heating is effected directly through the jacket of the reactor chamber and by preheating the steam.

This system allows - at least via the inlet bottom - to operate at very high water vapor partial pressures. but,
Excessively strong large bubble formation (゛′
bypass flow #) and therefore have to work with extremely excessive amounts of steam. In addition, a thermal profile/resistance is required which is additionally influenced by indirect heating corresponding to the high external temperature of the reaction wall.

The subject of the invention is a method for carrying out gas/solid reactions, in particular for activating or reactivating activated carbon, which is characterized in that the reaction is carried out in a horizontal reaction chamber with an oscillating flow. This is done inside the floor.

Activation and reactivation of activated carbon is carried out with steam or other oxidizing residues, such as neified carbon, air, etc. Activation gas is reaction waste gas in heat exchanger at 400~8o
According to the invention, the activation is carried out in the following temperature ranges: Steam temperature: 60o to 800oC Fluidized bed temperature: 60o to 950oC Cass body temperature: 950 to 1200oC Heating of the reaction chamber takes place in a direct manner.

That is, such heated gas is heated in a countercurrent manner or in a coking coal bed
It is guided in parallel with t+:.

The heating gas can be, for example, generated by burning a propane/air mixture. Other heating gases or liquid fuels such as fuel oil or tar can also be used.

The reaction chamber waste during activation is thereby guided so that the coking coal is pretreated.

This pretreatment of coking coal is carried out by converting the coking coal, coking and/or pre-oxidizing the coal into a vibrating fluidized bed groove.
ζ Spoon done while loading.

In this case, the loading of the raw coal takes place in such a way that the raw coal is fed into the hopper by means of a metering device, for example a metering screw. In this case, the surrounding area of the popper is washed with reaction waste gas.

In a further embodiment, it is possible for the arrangement of the raw coal to take place by means of vibrating grooves which are optionally provided in the reaction waste gas line.

In another embodiment, the drying of the coking coal is carried out after loading into the back of a vibrating fluidized bed, in which case the chamber is divided below the flow nozzle, and the reaction takes place in the first part. At least a portion of the waste gas is introduced and passed through the coking coal.

To assist in the activation, secondary air is introduced into the reaction chamber through one or more lances, which are provided parallel to the vibrating fluidized bed grooves and have a large number of holes. .

Once the reaction has proceeded, heating the needle can be carried out solely by supplying secondary air.

The secondary air is heated to 200-500% by the reaction waste gas in the heat exchanger.
A temperature of 0° is preheated to 6°. Another object of the invention is an apparatus for carrying out the above method, which is characterized by a vibrating fluidized bed groove in the double jacket. is provided.

Inner one-tA, capital is insulated-jacket 3a
The three jackets that surround the burning waste body and mainly serve to reflect thermal radiation are subjected to a load up to the upper limit for a metal material according to the temperature (maximum 1200℃), so the jacket does not receive any mechanical load. Please be considerate. while the outer m-jacket 3b, which provides radiation protection in the inner jacket, receives all the static stresses;
Pi-riki is also performed to seal the inside of the furnace from the outside atmosphere.

A raw coal loading device is installed in the reaction waste gas line. .

Inside the double jacket 3 there is a secondary air lance 16 parallel to the vibrating fluidized bed groove 1 driven by the vibrating member 2.
There are some settings.

The vibrating IL moving bed groove 1 has two separate gas supply openings and l'
, +j 4'i and 18.

The method according to the invention as well as the installation according to the invention have in particular the following advantages:

The incoming piston flow of the reactants avoids non-uniform remixing, thereby achieving a short residence time spectrum.
L.

The cross-flow of the fluidizing gas ensures a high ice-fish partial pressure within the carbonaceous bed and a rapid uplift of inhibiting products such as hydrogen and carbon monoxide.

The invention will be explained in more detail below with reference to embodiments illustrated in the accompanying drawings.

In FIG. 1, the apparatus according to the invention includes a vibrating fluidized bed groove 1,
Supply is carried out from the vibrating drive unit 2 of the vibrating fluidized bed groove 1, the double jacket 3 surrounding the vibrating fluidized bed groove 1, and the metering screw 5. from the product outlet 6, the burner 7, the waste gas opening 8 and the steam supply device 9 within.

The raw coal 20 is fed into the hopper-like pellet loading section 4 by the wiring screw 50 and falls into the vibrating fluidized bed section 1-1. The reaction waste gas 21 is led in the opposite direction along the coking coal bed/biased section 4 to the waste gas opening 8 to form the activated carbon material 20'.
falls through the product discharge opening 6 into the storage container 10.

The steam necessary for the reaction is supplied to the coking coal 2 by a steam supply device 9.
The reactants are introduced into the vibrating fluidized bed groove 1 through the inlet bottom 11 below 0 and into the reactant.

As shown in FIG. 2, the raw coal 20 is placed in the raw coal loading section 4 via the vibrating groove 12. This vibration groove 12 is connected to the motor 16
This vibrating groove 12 is driven by the
The reactor is heated by the reaction waste gas at the top. The raw coal is placed in the varnish screw 14 through the vibration groove 12-
Loaded into L.

A secondary air lance 16 is additionally provided in the reaction chamber 15 parallel to the vibrating fluidized bed groove 1.5 As shown in FIG. The flow is arranged in such a way that there is a countercurrent flow to the raw coal flow, so that the supplied swept air is guided countercurrently to the reactants. Raw coal is directly loaded into the vibrating fluidized bed groove 1 by the raw coal loading device 4 . The activated carbon is carried out in a vibration cooler 17, where the reactants are cooled to below the reaction temperature.

As shown in FIG. 4, the vibrating fluidized bed section 1 is divided into two parts by a wall 18. In section 1a, the reaction waste gas is introduced into the coking coal through the inlet bottom 11. This dries the coking coal.

Steam is supplied in the section 16 of the vibrating fluidized bed groove 1.

According to FIG. 5, a vibrating fluidized bed groove 1 with an inlet bottom 11 is provided in the center of the two-wheeled jacket 3. A secondary air lance 16 is provided parallel to and above the vibrating fluidized bed groove 1 .

The method according to the invention is explained in more detail in the following example.

Total 1) Reactivation of loaded lignite coke used for wastewater purification.

2) 1 - raw material, 2 = product: n, b - indeterminate 5) Pensol loading is the carbonaceous material at 20 °C and constant pensol partial pressure (p
/po) in the amount of penzole that is absorbed.

4) Determined by DAB6.

5) Sugar density number: constant under standard conditions - amount of carbon material/I1%F that achieves the same coloring efficiency as activated carbon.

6) Carbon material t temporally gasified with respect to the fluidized bed surface:

[Brief explanation of the drawing]

1 is a longitudinal sectional view of the device according to the invention, FIG. 2 is a longitudinal sectional view of another configuration of the device according to the invention with a coal preheating device, and FIG. 3 is a longitudinal sectional view of another configuration of the device according to the invention with a coal preheating device; Fig. 4 is a longitudinal sectional view of another apparatus according to the invention incorporating a secondary air lance and a carbon preheater in a vibrating fluidized bed; 1 is a cross-sectional view of the apparatus according to the present invention. Reference numbers in the figure are 1... Vibrating fluidized bed groove 2... Vibrating device 3... Double jacket 16... Secondary air lance 18... Partition wall No. Figure 1 Figure 2

Claims (1)

[Claims] 1. A method for carrying out gas/'solid-state reactions, in particular for activating and reactivating activated carbon, in which the reaction is carried out in an oscillating fluidized bed provided in a horizontal reaction chamber. The above method is characterized by: 2. The method according to claim 1, wherein the activated carbon is activated and reactivated in steam or other oxidizing scum. 6. Activate residue in heat exchanger with reaction waste gas at 400~8
3. A method according to claim 2, wherein the method is heated to a temperature of 0.000C. 4. The method according to claim 2 or 5, wherein the activation is carried out in the following temperature ranges: steam temperature 600 to 800°C, fluidized bed temperature 600 to 950°C, and waste body temperature 950 to 1200°C. . 5 Claims 1 to 4 characterized by a reaction chamber
The method described in any one of the preceding paragraphs. 6. The method according to claim 5, wherein the heating gas is introduced countercurrently to the flow n of coking coal. Z. A method according to claim 6, wherein the heating gas is conducted co-currently with the coking coal stream. 8. The method according to any one of claims 1 to 7, wherein raw coal is pretreated with reaction waste gas. 9. The method according to any one of claims 1 to 8, characterized in that secondary air is supplied in the reaction chamber auxiliary by one or more lances. 10. A method according to claim 9, wherein the secondary air is preheated in a heat exchanger to a temperature of 200 to 500<0>C. 11. The method according to claim 5 or 1 (9), in which the heating is carried out exclusively by supplying secondary air. 12. Vibrating flow in double jacket (13) Floor groove (
1) A device for carrying out the method according to claim 1, wherein: 1) is provided. 16. ii.(
equipment. 14. Vibrating fluidized bed groove (1) in double jacket (3)
) parallel to one or more secondary air lances (
16), wherein the vibrating fluidized bed groove is provided with two separate gas supply openings and a septum (18). The device according to item t.